The method of obtaining polymers butadienestyrene

 

(57) Abstract:

The invention relates to the field of production butadienestyrene polymers. The method of obtaining butadienestyrene (co)polymers by solution or emulsion polymerization of 1,3-butadiene and/or its copolymerization with co monomer in the presence of catalyst(s) polymerization of one or more polymerization zones, followed by distillation of a mixture containing unreacted hydrocarbons WITH4and a selection of her more concentrated 1,3-butadienestyrene stream, which is returned to the polymerization zone, at the same time as butadienestyrene raw stream of a mixture of hydrocarbons WITH4containing predominantly 1,3-butadiene and 2-butenes in a ratio of 1:1 to 20:1, after the (co)polymerization greater part of 1,3-butadiene produce a hydrocarbon mixture, comprising predominantly 2-butenes and 1,3-butadiene, which is subjected to separation by distillation in at least one distillation zone, where distilled concentrate of 1,3-butadiene containing 5 - 50% 2-butenes, from VAT residue, in which the proportion of 2-butene and 1,3-butadiene exceeds 2:1, preferably greater than 20:1, and the specified butadiene concentrate is directed to areas of the CSOs from commodity flows by copolymerization) butadienestyrene mixture, comprising mainly of 1,3-butadiene and 2-butenes, without applying for subsequent concentration and recycling of 1,3-butadiene complex processes with selective separating agents. 11 C.p. f-crystals, 7 tab., 5 Il.

The invention relates to the field of production butadienestyrene polymers.

More specifically the invention relates to methods for butadienestyrene polymers with subsequent concentration and recirculation neprevyshenie 1,3-butadiene.

Known methods for producing polybutadiene rubbers and copolymers of 1,3-butadiene with comonomers by polymerization in the presence of catalysts of various types, including alkaline metals (sodium, potassium), systems containing ORGANOMETALLIC halide and metal compounds (hereinafter referred to in the formulas, R is a hydrocarbon radical, n is the number of atoms):

LiR, "TiClnI4-n+lR3",

"With(R)3+lRnCL3-n+H2O",

"rare earth metal

(COOR)n+AlRnCl3-n+AlRnH3-n"

(for example N(R)3+AlRCl2+AlR2H).

The composition of the catalytic systems may include substances donor, such as methyl ether of diethylene glycol. In most kuchmiy and technology of synthetic rubber. L.: Chemistry, 1970, S. 286-335, 361-365].

There are also known methods for producing copolymers of 1,3-butadiene with styrene, -methylstyrene, Acrylonitrile and other monomers by emulsion polymerization [P. A. Kirpichnikov and other Album of technological schemes of the main industries of the UK. L.: Chemistry, 1986, S. 173].

When using existing methods for 1,3-butadiene sent to the curing area (or the area of preparation of the mixture for polymerization), there are very strict requirements on its concentration, namely the Russian industry standard: not less than 99% 1,3-butadiene for stereoregular polymerization of polybutadiene in the rubber and not less than 98% 1,3-butadiene for emulsion polymerization, usually used for the co-polymerization of 1,3-butadiene with other monomers: styrene, a-methylstyrene, Acrylonitrile, etc.

The conversion of 1,3-butadiene in the polymerization is in the range from 60 to 90% [P. A. Kirpichnikov and other Album of technological schemes of the main industries of the UK. L.: Chemistry, 1986, S. 141, 175-176]. After polymerization is separated hydrocarbon stream containing predominantly 1,3-butadiene, much of which is recycled to the polymerization zone. In ibbean however, significant losses of 1,3-butadiene.

Known and most similar to that proposed by us is described in the book: O. C. Litwin. The basic technology of synthetic rubbers. M: Goskomizdat, 1959, S. 220-221, 345-445, the method of obtaining butadienestyrene polymers by polymerization of 1,3-butadiene and/or its mixtures with other monomers in the presence of catalyst(s) polymerization and possibly inert solvent in one or more polymerization zones, followed by distillation of a mixture containing unreacted hydrocarbons WITH4and the release of her enriched 1,3-butadiene stream by selective separating agent, for example water-ammonium acetate solution of monovalent copper, with the subsequent return it to the zone(s) polymerization.

A serious disadvantage of this method is its complexity (see Fig. 62 in this book O. C. Litwin) and high energy intensity. The application for the concentration of 1,3-butadiene other selective separating agents (acetonitrile, dimethylformamide, N-methylpyrrolidone) and for a concentration in technological version of extractive distillation [S. Y. Pavlov and other Processes of isolation and purification of butadiene. M: Tsniiteneftehim, 1971], but in this case, the process end is containing (co)polymers by solution or emulsion polymerization of 1,3-butadiene and/or its copolymerization with co monomer in the presence of a polymerization catalyst in one or more polymerization zones with subsequent distillation of the mixture, containing unreacted hydrocarbons4and a selection of her more concentrated 1,3-butadienestyrene stream, which is returned to the polymerization zone, at the same time as butadienestyrene raw stream of a mixture of hydrocarbons WITH4containing predominantly 1,3-butadiene and 2-butenes in a ratio of from 1:1 to 20:1, after the (co)polymerization greater part of 1,3-butadiene produce a hydrocarbon mixture, comprising predominantly 2-butenes and 1,3-butadiene, which is subjected to separation by distillation in at least one distillation zone, where distilled concentrate of 1,3-butadiene containing from 5 to 50% of 2-butenes from VAT residue, in which the proportion of 2-butene and 1,3-butadiene exceeds 2:1, preferably greater than 20:1, and the specified butadiene concentrate is directed to the curing area.

As a variant it is proposed a method in which as raw butadienestyrene flow of a mixture of hydrocarbons WITH4containing predominantly 1,3-butadiene and 2-butenes in a ratio of from 4:1 to 12:1.

As a variant it is proposed a method in which as raw butadienestyrene flow of a mixture of hydrocarbons WITH4in which you provide is containing a series of predominantly 1,3-butadiene and 2-butenes, distilled concentrate of 1,3-butadiene containing from 25 to 50% of 2-butenes, and at the entrance to the curing area support relative concentration of 2-butenes from 8 to 50% on the amount of 1,3-butadiene and 2-butenes, coming from raw materials and recycled butadienestyrene streams4.

As a variant it is proposed a method in which as raw butadienestyrene flow of a mixture of hydrocarbons WITH4in which the content of 2-butene in the form of TRANS-2-butene is less than 1.5%, preferably not more than 0.3%, and if selected after rectification (co)polymerization of a mixture containing predominantly 1,3-butadiene and 2-butenes, distilled concentrate of 1,3-butadiene containing from 5 to 25% 2-butenes, and at the entrance to the curing area support relative concentration of 2-butenes from 5 to 35% on the amount of 1,3-butadiene and 2-butenes in the raw materials and recycled butadienestyrene threads WITH4.

As a variant it is proposed a method in which after the (co)polymerization produce a hydrocarbon mixture comprising 2-butenes, 1,3-butadiene and optionally hydrocarbons having normal boiling points below -6oWith, and when her separation by distillation is distilled off, the mixture having a high content of carbohydrate is less than 50%, output VAT residue, in which the proportion of 2-butene and 1,3-butadiene exceeds 5:1, preferably greater than 20: 1, and produce a concentrate of 1,3-butadiene containing from 20 to 50% 2-butenes, which may further purified from traces recycle to the polymerization zone.

As a variant it is proposed a method in which when selected after rectification (co)polymerization of a hydrocarbon mixture from the bottom to the output stream, containing mainly 2-butenes, and additionally top output stream having a high content of hydrocarbons having normal boiling points below -6oAnd as a side selection deduce concentrate 1,3-butadiene.

As a variant it is proposed a method in which separation is allocated after the (co)polymerization of a hydrocarbon mixture is carried out in two distillation zones, the first of which effect the Stripping mixture having a high content of hydrocarbons having normal boiling points below -6oAnd the second effect the Stripping concentrate 1,3-butadiene from the cubic residue containing mainly 2-butenes.

As a variant it is proposed a method in which at least one polymerization zone, the polymer is th atom of aluminum or lithium, after the (co)polymerization produce a mixture comprising 1,3-butadiene, 2-butenes and isobutane and/or isobutene and rectification optionally distilled off the mixture with a high content of isobutane and/or isobutene, output VAT residue with a predominant content of 2-butene(s) and produce a concentrate of 1,3-butadiene, and returned to the curing area.

As a variant it is proposed a method in which zone(s) distillation of hydrocarbon mixtures WITH4allocated after the (co)polymerization, at the same time serves the original butadienestyrene commodity flow output as VAT residue stream with a high content of 2-butenes, it is also possible to suppress the flow with a high content of hydrocarbons having a normal boiling point below -6oWith, and the obtained concentrate 1,3-butadiene is sent to the curing area.

As a variant it is proposed a method in which the conversion of 1,3-butadiene contained in the feed stream in a mixture of 2-butenes, are conducted sequentially in at least two polymerization zones, in at least the first of which carry out the polymerization of 1,3-butadiene into polybutadiene rubber and at least part of the allocated after the mixture containing nerror the(s) 1,3-butadiene with other monomer(s), such as styrene, and the concentration of 1,3-butadiene by distillation carried out between the said polymerization zones and/or zone specified additional (co)polymerization.

As a variant it is proposed a method in which butadienestyrene commodity flow and/or mixture butadienestyrene raw stream and recirculated condensate of 1,3-butadiene and/or a mixture butadienestyrene raw stream and a hydrocarbon mixture WITH4allocated after polymerization, purified from traces-acetylene hydrocarbons and oxygen-containing compounds.

Alternatively proposed a method that allows for the removal of trace contaminants spend interaction with aluminization(s) and/or aluminosilicates(s) with subsequent distillation of the treated hydrocarbons.

The proposed method can be used as feed stream to the polymerization (or one of the flows of raw material by copolymerization) butadienestyrene mixture comprising predominantly 1,3-butadiene and 2-butenes, without applying for subsequent (after polymerization) concentration and recycling of 1,3-butadiene complex processes with selective separating agents. Near the years of 2-butenes and the subsequent concentration of 1,3-butadiene (separating it from part 2-butenes) by distillation, held by distillation and subsequent recycling to the polymerization zone) butadiene concentrate containing from 5 to 50% 2-butenes (calculated on the amount of 1,3-butadiene and 2-butenes), preferably from 5 to 35% of 2-butenes, if the raw stream contains no more than 1.5% of TRANS-forms of 2-butene. When the specified condition relative volatility of 1,3-butadiene and 2-butenes is sufficient for rectification with a small consumption of power.

The polymerization can be carried out using various polymerization available technologies and catalysts, such as processes stereoregular polymerization in solution in the presence of ORGANOMETALLIC catalysts, processes of emulsion polymerization and copolymerization, etc. may Also be used various available methods of separation of mixtures containing mainly hydrocarbons WITH4(mainly 1,3-butadiene and 2-butenes) from mixtures resulting from polymerization. It is essential that the concentration of 1,3-butadiene using the techniques set forth in the claims.

In some polymerization processes (usually when using the catalyst composition triisobutylene education isobutene, and/or isobutane, and/or propene and/or propane, so allocated after polymerization mixture in addition to 1,3-butadiene and 2-butenes can contain these hydrocarbons having normal boiling points below -6oWith, even if they were not in raw butadienestyrene thread. If allocated after polymerization mixture containing predominantly 1,3-butadiene and 2-butenes, also includes hydrocarbons having normal boiling points below -6oWith, the process can include additional distillation of these hydrocarbons.

The use of the invention is illustrated in Fig.1-5 and examples. These drawings and examples do not exhaust all possible options for the use of the invention and possible other technological options, while respecting the fact set forth in the claims.

According Fig. 1 source butadienestyrene mixture of hydrocarbons WITH4F (stream 1), the flow of recirculated concentrate 1,3-butadiene (together they form the thread 2), a solution of catalyst(s) (stream 3), and possibly other components (stream 4) is fed to the polymerization zone. Thread 5 from the polymerization zone is sent to the separation zone of polymerizate where deduce the polymer (stream 6), possibly on ntification column or subjected To purification from harmful for the polymerization of trace contaminants in the area of Ω, from which column To direct the flow 9.

From the bottom of the column To display the VAT residue with a high content of 2-butenes (stream 10), and the top of the column To bring the concentrate 1,3-butadiene (stream 11), which recycle to the polymerization zone.

The diagram in Fig.2 differs from the Fig.1 in that the hydrocarbons4from the separation zone of polymerizate (stream 7) is served in a distillation column, from which derive three streams: lower - VAT residue with a high content of 2-butenes (stream 10), top the mixture with a high content of light hydrocarbons having a normal boiling point below -6o(Stream 9), and side - concentrate 1,3-butadiene (stream 11), which recycle at the site of polymerization.

The diagram in Fig.3 differs from the Fig.1 and 2 in that the hydrocarbons4from the separation zone of polymerizate (stream 8) is served in a distillation column K-1, above which display a mixture with a high content of light hydrocarbons having a normal boiling point below -6o(Stream 9), and the bottom output stream 9a, which is sent to distillation column K-2.

From the bottom of column K-2 output VAT residue with a high content of 2-butenes (stream 10) and the top place containerization serves the concentrate stream of 1,3-butadiene, recycled from the distillation column K-2, a solution of catalyst (stream 3), and possibly other components (non-hydrocarbons WITH4) (stream 4).

Thread 5 from the polymerization zone is fed to the separation zone of polymerizate, from which derive the polymer (stream 6), possibly other components (non-hydrocarbons WITH4) (stream 7) and hydrocarbons WITH4(stream 8). Stream 8 is fed to the rectification. Simultaneously with the thread 8 on the rectification of serves the initial mixture of hydrocarbons WITH4(thread 1).

Rectification is carried out either in a column K-2, where it receives respectively the threads 1A and 8A, either initially in the column K-1, where flows 8 and you can stream 1B. Top K-1 column (if used) output stream with a high content of light hydrocarbons (stream 9) and the lower thread 8B, served in the column K-2.

From the bottom of column K-2 output VAT residue with a high content of 2-butenes (stream 10), and the top hatch concentrate 1,3-butadiene (stream 11), which is sent to the curing area. Before serving in the curing area stream 11 may be subjected to purification from harmful for the polymerization of trace contaminants in the area of Ω, where that will stream 12, and then supplied to the node p is for the polymerization zone and the separation zone of polymerizate. In the first node of polymerization and separation polymerizate (node 1) submit the original butadienestyrene F (stream 1), may be recycled to the concentrate stream of 1,3-butadiene (stream 18) (together forming stream 2), a solution of catalyst(s) (stream 3), and possibly other components (non-hydrocarbons WITH4) (stream 4).

Thread 7, if it contains a significant amount of "light" hydrocarbons with boiling points below -6oWith, send in a distillation column K-1. If "light" hydrocarbons are absent or their content is not relevant, the thread 7 is sent to the column K-2 (line 7A or 8A) and/or node 2 polymerization and separation polymerizate (along the lines 8B and 12). Top K-1 column (if used) output stream 9 with a high content of light hydrocarbons. Bottom output stream 8 which is sent to the column K-2 and/or node 2.

From the bottom of column K-2 output stream 10 with a high content of 2-butenes, and the top - concentrate 1,3-butadiene (stream 11). Stream 11 is sent to node 2 polymerization and separation polymerizate on lines 11B and 12 and/or recycle at node 1 along lines 11A or 18.

In node 2 serves also a solution of the catalyst (stream 13) and possibly other components (stream 14).

< / the flow of hydrocarbons FROM4(line 17) which is sent to the column K-1 on line 19 and/or the node 1 through line 18, and/or removed from the process (line 20). The scheme is used so that the column K-2 must be served on the separation of at least one of the threads 8A and 19.

In K-2 (or original in K-1 and then K-2) may be filed with the flow source butadienestyrene mixture F (stream 1A).

EXAMPLE 1.

The process is executed according to Fig.1.

Spend emulsion copolymerization of 1,3-butadiene with styrene at a ratio in the feed to the polymerization mixture 2:1, a temperature of 50oC, the ratio of monomers : water 1:1,25 (wt.). As an inhibitor of polymerization using potassium persulfate as a regulator of the molecular weight of tert-dodecylmercaptan, as an emulsifier is a mixture of potassium salts of fatty acids, as the stopper - dimethyldithiocarbamate.

After polymerization and separation of the reaction mixture get the best choice of the polymer in the amount of 0.70 kg per 1 kg of raw 1,3-butadienestyrene mixture F.

Description of the key WITH4streams and main technological parameters are given in table.1.

EXAMPLE 2.

The process is executed according to Fig.1.

oAnd the ratio of monomers : water 1:2,1 (wt.). As an inhibitor of polymerization of the use of cumene hydroperoxide (0.2% of the mixture), as the regulator of the molecular weight of tert-dodecylmercaptan (0,2%), as an emulsifier potassium soap disproportionating rosin, as the stopper - dimethyldithiocarbamate sodium.

After polymerization and separation of the reaction mixture get the best choice of the polymer in the amount of 1.35 kg per 1 kg of raw 1,3-butadienestyrene mixture F.

Feature WITH4streams and main technological parameters is given in tab.2.

EXAMPLE 3.

The process is executed according to Fig.2.

Carry out solution polymerization of 1,3-butadiene into polybutadiene rubber at a concentration of 12% 1,3-butadiene in solution and a gradual increase in temperature from 5 to 30oC. In the solvent used toluene as the catalytic system system TiI2Cl2+ triisobutylaluminum. After polymerization, the catalytic complex decompose 1% solution of KOH.

After polymerization and separation of the reaction mixture get 0.64 kg of polymer per 1 kg of raw 1,3-butadienestyrene see the>EXAMPLE 4.

The process is executed according to Fig.3.

Carry out solution polymerization of 1,3-butadiene to CIS-polybutadiene rubber in conditions similar to those specified in example 3 (but with a different content of 2-butenes).

After polymerization and separation of the reaction mixture get 0,91 kg of polymer per 1 kg of raw 1,3-butadienestyrene mixture F.

Feature WITH4streams and main technological parameters is given in tab.4.

EXAMPLE 5.

The process is executed according to Fig.3.

Carry out solution polymerization of 1,3-butadiene to CIS-polybutadiene rubber in conditions similar to those specified in example 3 (but with a different content of 2-butenes).

After polymerization and separation of the reaction mixture get 0,91 kg of polymer per 1 kg of raw 1,3-butadienestyrene mixture F.

Feature WITH4streams and main technological parameters is given in tab.5.

EXAMPLE 6.

The process is executed according to Fig.4.

Carry out solution polymerization of 1,3-butadiene to CIS-polybutadiene rubber in conditions similar to those specified in example 3 (but with a different content of 2-butenes).

Raw 1,3-butadienestyrene polymerization and separation of the reaction mixture get 0.70 kg of polymer per 1 kg of raw 1,3-butadiene mixture F.

Feature WITH4streams and main technological parameters is given in tab.6.

EXAMPLE 7.

The process is executed according to Fig.5 according to the scheme, including the supply of raw 1,3-butadienestyrene mixture F on lines 1 and 2 in curing the node 2, the feed stream 7 in column K-1 (from which the output stream 9), flow 8 in column K-2 (from which the output stream 10), flow 11 in curing the node 2 on the lines 11, 11B and 12 and the recirculation of the output node 2 of the flow of hydrocarbons FROM4in column K-1 on lines 17 and 19.

In node 1 carry out the polymerization of 1,3-butadiene (in the presence of 2-butenes) in the CIS-polybutadiene rubber. Used catalysts, solvent, temperature and method of catalytic decomposition of the complex is similar to that described in example 3.

In node 2, carry out emulsion polymerization of 1,3-butadiene together with is supplied to the node with styrene. Used in the site catalysts, auxiliary substances and process parameters such as the one outlined in example 2.

The conversion of 1,3-butadiene per pass in node 1 is 70%, site 2 - 80%. In node 1 receive polybutadiene rubber in the number 0,63 kg/kg F, node 2 is the best choice of the polymer in a quantity

1. The method of obtaining butadienestyrene (co)polymers by solution or emulsion polymerization of 1,3-butadiene and/or its copolymerization with co monomer in the presence of catalyst(s) polymerization of one or more polymerization zones, followed by distillation of a mixture containing unreacted hydrocarbons WITH4and a selection of her more concentrated 1,3-butadienestyrene stream, which is returned to the polymerization zone, at the same time as butadienestyrene raw stream of a mixture of hydrocarbons WITH4containing predominantly 1,3-butadiene and 2-butenes in a ratio of 1: 1 to 20 : 1, after the (co)polymerization greater part of 1,3-butadiene produce a hydrocarbon mixture, comprising predominantly 2-butenes and 1,3-butadiene, which is subjected to separation by distillation in at least one distillation zone, where distilled concentrate of 1,3-butadiene containing 5 - 50% 2-butenes, from VAT residue, in which the proportion of 2-butene and 1,3-butadiene exceeds 2 : 1, preferably greater than 20 : 1, and the specified butadiene concentrate is directed to the curing area.

2. The method according to p. 1, wherein the resource butadienestyrene flow of a mixture of coal is about on p. 1, where as raw butadienestyrene flow of a mixture of hydrocarbons WITH4in which the content of 2-butene in the form of TRANS-2-butene exceeds 1.5%, and if selected after rectification (co)polymerization of a mixture containing predominantly 1,3-butadiene and 2-butenes, distilled concentrate of 1,3-butadiene containing 25 - 50% 2-butenes, and at the entrance to the curing area support relative concentration of 2-butenes in the range 8 - 50% on the amount of 1,3-butadiene and 2-butenes, coming from raw materials and recycled butadienestyrene streams4.

4. The method according to p. 1, wherein the resource butadienestyrene flow of a mixture of hydrocarbons WITH4in which the content of 2-butene in the form of TRANS-2-butene is less than 1.5%, preferably not more than 0.3%, and if selected after rectification (co)polymerization of a mixture containing predominantly 1,3-butadiene and 2-butenes, distilled concentrate of 1,3-butadiene containing 5 - 25% 2-butenes, and at the entrance to the curing area support relative concentration of 2-butenes in the range of 5 to 35% on the amount of 1,3-butadiene and 2-butenes in the raw materials and recycled butadienestyrene threads WITH4.

5. The method according to p. 1, wherein after (with)p is normalname boiling points below -6oWith, and when her separation by distillation is distilled off, the mixture having a high content of hydrocarbons having normal boiling points below -6oWith and preferably having a content of 1,3-butadiene is less than 50%, output VAT residue, in which the proportion of 2-butene and 1,3-butadiene exceeds 5 : 1, preferably greater than 20 : 1, and produce a concentrate of 1,3-butadiene containing 20 - 50% 2-butenes, which may further purified from traces recycle in the area(s) polymerization.

6. The method according to p. 5, in which when selected after rectification (co)polymerization of a hydrocarbon mixture from the bottom to the output stream, containing mainly 2-butenes, and additionally top output stream having a high content of hydrocarbons having normal boiling points below -6oAnd as a side selection deduce concentrate 1,3-butadiene.

7. The method according to p. 5, wherein the separation allocated after the (co)polymerization of a hydrocarbon mixture is carried out in two distillation zones, the first of which effect the Stripping mixture having a high content of hydrocarbons having normal boiling points below -6oAnd the second effect the Stripping concentrate 1,3-buta is AK at least one polymerization zone, the polymerization is carried out in the presence of compound(s), comprising(a) at least one isobutylene group bonded to an atom of aluminum or lithium, after the (co)polymerization produce a mixture comprising 1,3-butadiene, 2-butenes and isobutane and/or isobutene and rectification optionally distilled off the mixture with a high content of isobutane and/or isobutene, output VAT residue with a predominant content of 2-butene(s) and produce a concentrate of 1,3-butadiene, and returned to the curing area.

9. The method according to p. 1, characterized in that the zone(s) distillation of a hydrocarbon mixture WITH4allocated after the (co)polymerization, at the same time serves the original butadienestyrene commodity flow output as VAT residue stream with a high content of 2-butenes, it is also possible to suppress the flow with a high content of hydrocarbons having a normal boiling point below -6oWith, and the obtained concentrate 1,3-butadiene is sent to the curing area.

10. The method according to p. 1, wherein the conversion of 1,3-butadiene contained in the feed stream in a mixture of 2-butenes, are conducted sequentially in at least two polymerization zones, in at least the first of which carry out the polymerization of 1,3-butadiene into polybutadiene kaoclay additional (co)polymerization in the polybutadiene or a copolymer(s) of 1,3-butadiene with other monomer(s), such as styrene, and the concentration of 1,3-butadiene by distillation carried out between the said polymerization zones and/or zone specified additional (co)polymerization.

11. The method according to p. 1, wherein butadienestyrene commodity flow and/or mixture butadienestyrene raw stream and recirculated condensate of 1,3-butadiene and/or a mixture butadienestyrene raw stream and a hydrocarbon mixture4allocated after polymerization, purified from traces-acetylene hydrocarbons and oxygen-containing compounds.

12. The method according to p. 11, wherein for removal of trace contaminants spend interaction with aluminization(s) and/or aluminosilicates(s) with subsequent distillation of the treated hydrocarbons.

 

Same patents:

The invention relates to the selection of synthetic rubber from latex and can be used in the manufacture of synthetic rubbers

The invention relates to a technology for syndiotactic 1,2-polybutadiene content of the vinyl groups of more than 85% and a crystallinity of 20 to 50% and can be used in the IC industry, rubber, Shoe, light, tire industry

The invention relates to the field of production of rubber for the manufacture of tyres, rubber, bitumen modification

The invention relates to the production of rubbers for the production of tires with high performance

The invention relates to the field of technology of macromolecular compounds, namely a process for the production of stereoregular Polivanov under the influence of the catalytic systems of the Ziegler-Natta

The invention relates to the field of production of rubber emulsion polymerization based on butadiene

The invention relates to the technology of CIS-1,4-polybutadiene and CIS-1,4-butadiene copolymer of isoprene under the influence of the catalyst systems of the Ziegler-Natta and can be used in the synthetic rubber industry

The invention relates to the technology of CIS-1,4-polybutadiene and CIS-1,4-copolymer of butadiene with isoprene and can be used in the synthetic rubber industry

The invention relates to techniques for stereospecific polymerization of butadiene-1,3 in obtaining high molecular weight stereoregular of copolyvidone used in tire, rubber, cable industry and other sectors of the economy

The invention relates to the technology of (co)polymers of conjugated dienes

The invention relates to a method for rubber
The invention relates to the synthetic rubber industry, and in particular to methods of producing CIS-1,4-polybutadiene polymerization of butadiene-1,3 in the environment of the hydrocarbon solvent under the action of a catalyst containing a compound of cobalt, alkylalkoxysilane and water, using low temperature processing components

The invention relates to the production of copolymers of dienes used in the manufacture of tyres

The invention relates to the technology of CIS-1,4-polybutadiene and CIS-1,4-butadiene copolymer of isoprene under the influence of the catalyst systems of the Ziegler-Natta and can be used in the synthetic rubber industry, and the resulting polymers in the rubber and tire industries

The invention relates to the field of production of emulsion rubbers, in particular copolymers of butadiene, vinylidene chloride with Acrylonitrile, and can be used in the manufacture of rubber products, working in the environment of fuels and oils, and non-flammable rubber products, in particular in the cable industry

The invention relates to the production of synthetic rubbers, in particular, to improve the stability of the rubber in terms of termostate

The invention relates to the production of emulsion rubbers and can be used for separation of rubber from latex
The invention relates to methods for producing socialization for the polymerization of butadiene, occurring in the presence of cobalt containing catalysts, and may find application in the IC industry in the production of CIS-1,4-polybutadiene
Up!